US3898857A - Process for regulating the quantity of cold delivered by a refrigerating installation - Google Patents

Process for regulating the quantity of cold delivered by a refrigerating installation Download PDF

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US3898857A
US3898857A US399279A US39927973A US3898857A US 3898857 A US3898857 A US 3898857A US 399279 A US399279 A US 399279A US 39927973 A US39927973 A US 39927973A US 3898857 A US3898857 A US 3898857A
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stream
gaseous
pressure
refrigerating
expanded
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Jean Bourguet
Joseph Gauberthier
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TEAL PROCEDES L'AIR LIQUIDE ET TECHNIP DE LIQUEFACTION DES GAZ NATURELS Ste
TEAL SOC
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TEAL SOC
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0212—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a single flow MCR cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B1/00—Compression machines, plants or systems with non-reversible cycle
    • F25B1/10—Compression machines, plants or systems with non-reversible cycle with multi-stage compression
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
    • F25B9/002—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant
    • F25B9/006—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant the refrigerant containing more than one component
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
    • F25J1/0055—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream originating from an incorporated cascade
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
    • F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0298—Safety aspects and control of the refrigerant compression system, e.g. anti-surge control
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream

Definitions

  • ABSTRACT There is provided a process and an installation, operating with an incorporated cascade cycle, in which there is at least one recycling flow drawn off from the cycle mixture at a high pressure the rate of flow of which is regulated, the arrangement being such that at least a part of the recycled flow is (i) expanded to a lower pressure, (ii) combined with a refrigerating stream undergoing evaporation, and (iii) recompressed together with the cycle mixture,
  • the invention is particularly applicable to the liquefaction of natural
  • This invention relates to refrigeration processes and. more particularly but not exclusively, is concerned with a process for regulating the quantity of cold delivered by a refrigeration installation which utilises the refrigerating cycle known as the incorporated cascade cycle.
  • the invention is particularly concerned with a refrigeration installation which makes it possible to cool, liquefy and possibly super-cool a gas, more particularly but not exclusively a natural gas.
  • a refrigeration installation operating the incorporated cascade cycle comprises, in general:
  • a compressor comprising a least one compression stage permitting the compression of at least one cycle mixture in gaseous form from a relatively low pressure to a relatively high pressure;
  • a condenser having an inlet which communicates with the output of the compressor, and which comprises means for circulating an external refrigerant, permitting at least the compressed cycle mixture to be partially condensed by heat exchange with the external refrigerant to give a first condensed fraction;
  • a heat exchange assembly comprising (a) a plurality of condensation pipes arranged in series the inlet of each of which communicates with the gas outlet of one separator and the outlet of each of which communicates with the inlet of the separator next in series, and (b) a vaporisation passages in heat exchange relationship with the condensation pipes, whereby in co-operation with the plurality of separators, fractional condensation of at least the gaseous remainder of the cycle mixture which has been separated from the first condensed fraction is effected at said high pressure while the remainder of the cycle mixture is circulating in said condensation pipes in heat exchange with, and countercurrently with respect to, a refrigerating stream constituting part of the cycle mixture which is passing through said vaporisation passage and is undergoing vaporisation at a vaporisation pressure at least equal to said low pressure, the plurality of separators permitting the collection and separation of further condensed fractions resulting from this fractional condensation;
  • a return pipe of which the upstream end communicates with said vaporisation passage and of which the downstream end communicates with a gas intake of the compressor which is at said vaporisation pressure, whereby there is effected the recompression to said high pressure of at least the vaporised refrigerating stream which constitutes part of the cycle mixture.
  • the external refrigerant ensuring the initial partial condensation of at least the compressed cycle mixture can either be water (for example, sea water) undergoing reheating, or a refrigerant (for example, propane) undergoing vaporisation, which has been previously compressed, condensed and expanded to a vaporisation pressure in a separate refrigerating cycle.
  • a refrigerant for example, propane
  • the refrigerating installation as previously described can use a refrigerating cycle of the open or closed type.
  • a closed cycle for liquefying for example, a natural gas
  • the natural gas circulates in a condensation passage disposed within the heat exchange assembly in heat exchange relationship with the vaporisation passage, but separate from the condensation pipes through which the cycle mixture flows.
  • the refrigerating stream of the cycle mixture is thus vaporised by heat exchange while flowing counter currently with respect to (i) the natural gas which itself is undergoing condensation, and (ii) the cycle mixture which is undergoing fractional condensation.
  • such a cycle operates at two separate vaporisation pressures, the first vaporisation pressure being that at which the cycle mixture is being vaporised by heat exchange with the cycle mixture undergoing fractional condensation, and the second vaporisation pressure being that at which the cycle mixture is being vaporised by heat exchange with a fluid from which it is desired to extract heat, such as a natural gas which is to be liquefied.
  • This cycle will hereinafter be called a two-pressure cycle.
  • the compressor comprises a first compression stage and a second compression stage, connected to one another by a connecting pipe under a pressure intermediate the low pressure and the high pressure, this making it possible for the cycle mixture to be compressed in two compression stages, separated by the intermediate pressure;
  • such a refrigeration installation comprises:
  • a second heat exchange assembly comprising a condensation passage in heat exchange relation with a vaporisation passage (hereinafter termed the second vaporisation passage), whereby the extraction of heat from an external fuid, or the condensation of, for example, a natural gas, is effected by heat exchange of the external fluid or of the natural gas, which is passing through said condensation passage, with a second refrigerating stream constituting part of the cycle mixture which stream is flowing through said vaporisation passage and is undergoing vaporisation at a vaporisation pressure substantially equal to the low pressure;
  • a refrigeration installation of the type just described delivers a quantity of cold which is distributed in accordance with a given temperature gradient.
  • the second refrigerating stream of the cycle mixture circulating in the second vaporisation passage within the second heat exchange assembly, supplied by its vaporisation and its progressive reheating from a cold temperature up to a hot temperature the quantity of cold which is necessary for cooling, condensing and possibly super-cooling the natural gas from the hot temperature to the cold temperature.
  • the compressor is generally a compressor of the axial or centrifugal type. It it is possible to cause a variation in the rate of flow of the cycle mixture which is drawn in, either by causing a variation in the speed of rotation of the compressor, or by modifying the position of the directional blades of the stator in the case of an axial compressor, the flexibility thus obtained is very limited.
  • the installation comprises in addition at least one recycling circuit comprising at least one variable delivery expansion device, of which the upstream side communicates with a gas outlet of the compressor means at a pressure at most equal to the high pressure, and of which the downstream side communicates with a gas inlet of the compressor at a lower pressure at least equal to the low pressure.
  • This recycling circuit is generally arranged around and in the intermediate proximity of the compressor, that is to say, in that part of the installation which is at ambient temperature.
  • an increase in the capacity of a liquefying installation for natural gas means that the power dissipated in the recycling circuit may be extremely large.
  • an installation which liquefies a nominal flow of 6500 cubic metres per day of liquid natural gas uses of the order of 66 megawatts of power for compression at the normal production rate, and 80 megawatts for maximum production rate.
  • the result of this is that, if a recycling circuit such as that described above is employed, the power dissipated in the recycling circuit can be extremely large.
  • the recycling circuit is consequently subjected to considerable vibration and the metal fatigue which results therefrom can very quickly lead to a breakdown in the equipment. This danger of breakdown is further accentuated by the following new problem.
  • At least one cycle mixture is compressed in gaseous form from a lowpressure to a high pressure, in at least one compression stage;
  • the compressed cycle mixture is partially condensed, by heat exchange with an external refrigerant, and a first condensed fraction is separated therefrom;
  • fractional condensation of at least the gaseous residual cycle mixture which has been separated from the first condensed fraction is carried out at said high pressure by heat exchange with, and while flowing counter-currently with respect to, a refrigerating stream which constitutes a part of the cycle mixture which stream is undergoing vaporisation at a vaporisation pressure at least equal to said low pressure, whereby a plurality of further condensed fractions is separated from the residual cycle mix- 6 ture; d. at least a part of each of the condensed fractions is expanded from said high pressure to said vaporisation pressure, and the expanded parts thus obtained are united with said refrigerating stream; and
  • the quantity of cold delivered by the installation is regulated by controlling the rate of flow of at least one recycling flow which is drawn off from the cycle mixture at a pressure at most equal to said high pressure, the arrangement being such that when the recycling flow takes place at least a part of the recycling flow is (i) expanded to a pressure substantially equal to said vaporisation pressure; (ii) combined with said refrigerating stream at a stage in the process not later than when said at least a part of the first condensed fraction, after having been expanded to said vaporisation pressure, is combined with the refrigerating stream; and (iii) recompressed together with the said refrigerating stream when the refrigerating stream has been vaporised.
  • the invention also provides a refrigerating installation which comprises:
  • a compressor comprising at least one compression stage permitting the compression of a cycle mixture in gaseous form from a relatively low pressure to a relatively high pressure;
  • a condenser having an inlet which communicates with the output of the compressor, and which comprises means for circulating an external refrigerant;
  • iii a plurality of separators arranged in series, each comprising an inlet, a liquid outlet and a gas outlet, the inlet of the first separator communicating with the outlet of the condenser;
  • a heat exchange assembly comprising (a) a plurality of condensation pipes arranged in series the inlet of each of the which communicates with the gas outlet of one separator and the outlet of each of which communicates with the inlet of the sepa' rator next in series, and (b) a vaporisation passage in heat exchange relationship with the said condensation pipes;
  • At least one recycling circuit comprising at least one adjustable flow expansion device, of which the upstream side communicates with a gas outlet of the compressor at a high pressure at most equal to said high pressure and of which the downstream side communicates with the gas intake of the compressor at a pressure at least equal to said low pressure, wherein the downstream side of the adjustable flow expansion device of the recycling circuit communicates with said vaporisation passage.
  • the recycling flow which has been expanded to the vaporisation pressure is combined with the refrigerating stream, at the latest when the latter has been combined with at least a part of the first condensed fraction after the first condensed fraction has been expanded to the vaporisation pressure. Consequently, in accordance with the invention, the downstream side of the expansion device of the recycling circuit communicates with the vaporisation passage reserved for the refrigerating stream undergoing vaporisation.
  • the invention provides the following advantages.
  • the junction between that part of the recycling circuit which is at the vaporisation pressure and the circuit of the refrigerating stream (i.e. the vaporisation passage and return pipe) which is also at the vaporisation pressure is moved back as far as possible into the cold part of the refrigerating installation, at least a part of the vaporisation passage and the return pipeare integrated into the recycling circuit.
  • a large part of the total mass of the installation thus participates in the dissipation of the vibrational energy resulting from the recycling.
  • the recycling circuit includes the last part of the vaporisation passage, in which the first condensed fraction is vaporised by heat exchange with the refrigeration stream, the dissipated thermal energy resulting from recycling is absorbed by the cycle mixture and is transferred by the latter, after compression, to the external refrigerant.
  • the dissipated thermal energy instead of directly reheating the installation, is recovered and methodically evacuated from the installation.
  • FIG. 1 shows diagrammatically an installation for liquefying natural gas, permitting the liquefaction of about 1 /2 thousand million cubic metres of natural gas per year, i.e about 187,000 cubic metres per hour (at n.t.p.) of natural gas, using a two-presence incorporated cascade cycle;
  • FIG. 2 represents the variations in the total delivery recycled around the compressor used in the installation shown in FIG. 1, as a function of the throughput of liquefied natural gas.
  • the refrigeration plant which is shown in FIG. 1 comprises first of all a compression device 1 (an axial compressor), driven by a steam turbine 2, which comprises a first compression stage 3 and a second compression stage 4 connected to one another by a connecting pipe 5 under an intermediate pressure (between the low pressure and the high pressure) at which the output of the stage 3 and the intake of the stage 4 function.
  • a refrigerator unit 6 is disposed on the connecting pipe 5.
  • a condenser 7 has an inlet communicating with the delivery side of the compression means 1 by means of a pipe 8 on which is disposed a refrigerating unit 9.
  • the condenser 7 comprises circulation means for an external refrigerant, such as water.
  • the inlet a of the first separator 10 communicates with the outlet of the condenser 7.
  • a first heat exchange assembly represented at 13, comprises a first exchanger 14 and a'second exchanger 15.
  • This heat exchange assembly 13 comprises a plurality of condensation pipes 16, 17 and 18 arranged in series.
  • the first pipe 16 is disposed in the exchanger 14, while the pipes 17 and 18 are disposed in the exchanger 15.
  • the inlet end of each condensation pipe bearing the appropriate reference number together with the index letter a, communicates with the gas outlet of a separator: the gas outlet with the inlet 16a, the gas outlet 1 1c with the inlet 17a and the gas outlet 12c with the inlet 18a.
  • the outlets of the first two condensation pipes 16 and 17 communicate with the inlets of the following separators: outlet 16]) with inlet 11a, outlet 17b with inlet 12a.
  • the heat exchange assembly 13 further comprises a vaporisation passage comprising the interior (grid side) of the exchanger 13, the connecting pipe 71 and the interior of the exchanger 14 (grid side) in heat-exchange relationship with the condensation pipes 16,17 and 18.
  • the installation comprises second heat exchange assembly 22, comprising a third exchanger 23 and a fourth exchanger 24.
  • This assembly comprises a condensation passage comprising a pipe 25 arranged within the exchanger 24, a connecting pipe 26 between the exchangers 23 and 24 and a pipe 27 arranged within the exchanger 23.
  • This condensation passage is in heat exchange relationship with a second vaporisation passage which is defined by the interior of the exchanger 23 (grid side), a connecting pipe 28 and the interior of the exchanger 24 (grid side).
  • the installation also comprises a first group of expansion devices in the form of valves 19, 20 and 21 and a second group of expansion devices in the form of valves 29, 30 and 31.
  • the upstream side of an expansion device communicates with the liquid outlet of a separator; thus liquid outlet 10b communicated with the expansion valve 19, liquid outlet 11b with the expansion valves 20 and 29 simultaneously, and liquid outlet 12b with the expansion valve 21 and the expansion valve 30 simultaneously.
  • the upstream side of the expansion valve 31 communicates with the outlet 18b of the condensation pipe 18 only.
  • the downstream side of each of the expansion valves 19, 20 and 21 communicates with the vaporisation passage of the first heat exchange assembly 13.
  • the downstream sides of the expansion valves 29, 30 and 31 communicate with the vaporisation passage of the second heat exchange assembly 22.
  • the upstream and downstream ends of a return pipe 32 communicate respectively with the vaporisation passage of the first heat exchange assembly 13 (more specifically with the interior of the exchanger 14) and with the inlet of the second compression stage 4 of the compressor which is under the intermediate pressure.
  • the upstream and downstream ends of another return pipe 33 communicate respectively with the vaporisation passage of the second heat exchange assembly 22 (more specifically with the interior of the exchanger 24) and with the intake of the compressor (that is, with the entry side of the first compression stage 3 at the low pressure).
  • the condensed fraction obtained from the initial, partial condensation of the cycle mixture is called the first condensed fraction, while the first of the further condensed fractions is called the second condensed fraction; subsequent further condensed fractions are given ascending ordinal numerical references so as to facilitate description.
  • a first part of a cycle mixture having an average molecular weight of 29 and comprising methane, nitrogen, ethane, propane, butane and pentane, arrives by way of the return pipe 33 and is compressed in gaseous form in the first compression stage 3 from a low presence of 1.5 at. to an intermediate pressure of 5.5 at. Then this first, compressed part, which has been cooled while at the intermediate pressure in the cooling unit or refrigerator 6, is further compressed in gaseous form in the second compression stage 4 to a high pressure of 38 at. together with a second part of the cycle mixture which has an average molecular weight of 34 and comprises the same constituents as the first part of the cycle mixture.
  • the second part of the cycle mixture arrives at compression stage 4 via return pipe 32.
  • the compression cycle mixture is thereafter cooled in the cooling unit 9, then partially condensed in the condenser 7, by heat exchange with an external refrigerant.
  • a first condensed fraction is then separated out from the cycle mixture in the first separator 10.
  • the whole of this first condensed fraction, amounting to 340 t/h, is then expanded in the expansion valve 19, and reunited with a refrigerating stream which is circulating inside the exchanger 14 (i.e. in the vaporisation passage of the first heat exchange assembly 13).
  • the fractionation takes place successively in the condensation pipes 16, 17 and 18, by heat exchange with, and counter-currently with respect to, a refrigerating stream circulating in the previously defined vaporisation passage, which stream is undergoing vaporisation at a vaporisation pressure which is substantially equal to the intermediate pressure (5.5 at.).
  • a second condensed fraction and a third condensed fraction are separated at, respectively, the outlet 16]; of the first condensation pipe 16 and the outlet 17b of the second condensation pipe 17; these two condensed fractions are collected in the second separator 11, at a temperature of -22C, and in the third separator 12, under a temperature of 80C, respectively.
  • a fourth condensed fraction, condensed at a temperature of -l30C, is not separated but is directly discharged from the upper part of the condensation pipe 18 located within heat exchanger 15.
  • a first part (170 t/h) and a second part (272 t/h) of the second condensed fraction which has been collected in the separator 11 are expanded respectively, to the intermediate pressure in the expansion valve 20 and to the low pressure in the expansion valve 29.
  • the first part of the second condensed fraction is reunited at intermediate pressure with the vaporised refrigerating stream circulating in the vaporisation passage of the first heat exchange assembly 13, and the second part of the second condensed fraction is reunited at the low pressure with the second refrigerating stream circulating in the vaporisation passage of the second heat ex change assembly 22.
  • the introduction of a part of the different condensed fractions into the vaporisation passage of the first heat exchange assembly 13 permits a refrigerating stream to be obtained which is undergoing vaporisation at the intermediate pressure while circulating in the said passage, in a vertical descending direction in the exchanger 15 and then in a vertical ascending direction in the exchanger 14.
  • This stream formed at the start by the first part of the third condensed fraction, then reunited successively with the first part of the second condensed fraction and with the first condensed fraction, is-vaporised and progressively reheated up to ambient temperature.
  • the introduction of a part of the different condensed fractions into the vaporisation passage of the other heat exchange assembly 22 permits another refrigerating stream to be obtained which is undergoing vaporisation at the low pressure while circulating in the second vaporisation passage in a vertical descending direction in the exchanger 23 and then in a vertical ascending direction in the exchanger 24.
  • This stream formed at the start by the whole of the fourth condensed fraction, then successively reunited with the second part of the third condensed fraction and with the second part of the second condensed fraction, is vaporised and is progressively reheated up to ambient temperature, by heat exchange in counter-current with natural gas being cooled, condensed and then supercooled from the ambient temperature down to a final cold temperature of about l62C, at a pressure of 42 at.,
  • the natural gas enters the installation through a line which joins the condensation pipe 25 within the exchanger 24, and then passes via line 26 to condensation pipe 27 within the exchanger 23.
  • the natural gas has the following composition:
  • the second refrigerating stream which has been undergoing vaporisation in the body of the second heat exchange assembly 22 passes via return pipe 33 to the compression stage 3 where it is recompressed from the low pressure to the intermediate pressure and then,
  • a first recycling circuit 34 comprising an adjustable flow expansion valve 38, of which the upstream side communicates with the gas outlet 12c of the separator 12, and consequently via the separators 10, 11 and 12 and the condensation pipes 16 and 17 with the high pressure gas outlet of the compressor 1, and of which the downstream side communi cates with the vaporisation passage of the assembly 13, more specifically with connecting pipe 71, and consequently via the final part of the vaporisation passage and the return pipe 32 with the intermediate pressure gas inlet of the compressor 1;
  • a second recycling circuit 35 comprising an adjustable flow expansion valve 39, of which the upstream side communicates with the gas outlet 12c of the separator 12, which is at the high pressure, and of which the downstream side communicates with the vaporisation passage of the second heat exchanger assembly 22, and more specifically with the lower part of the interior of the exchanger 23,
  • a third recycling circuit 36 comprising an adjustable flow expansion valve 40, of which the upstream side communicates with the pipe 8 between the cooling unit 9 and the condenser 7, which is at the high pressure, and of which the downstream side communicates with the lower part of the exchanger 14, which is at the intermediate pressure; and
  • a fourth recycling circuit 37 comprising a variable flow expansion valve 41, of which the upstream side communicates with the connecting pipe between the compression stages 3 and 4, which is at the intermediate pressure; and of which the downstream side communicates with the lower part of the exchanger 24, which is at the low pressure.
  • a stop recycling circuit 42 which includes an expansion valve 70
  • a stop recycling circuit 43 around the compression stage 3 which includes an expansion valve 44.
  • the pipes for these recycling circuits have a ratio between their radius and their thickness which is at most equal to 70.
  • FIG. 2 shows a plot of the quantity of natural gas to be liquefied (on the abscissae), expressed as a percentage of the nominal production of the installation, against the total recycled throughput (on the ordinates), expressed as a percentage of a reference throughput of the cycle mixture, which is that quantity delivered at the high pressure by the compressor 1 necessary for liquefying l07% of the nominal production of liquefied natural gas.
  • the solid line' on the plot relates to the first method of regulation (which is about to be described) while the dashed line relates to the second method of regulation which will be described later.
  • the installation delivers a quantity of cold corresponding to the functioning point R, (see FIG. 2), that is to say, to a production equal to 107% of the nominal production.
  • the power consumed by the compressor is 73.5 megawatts for a rotational speed of 3680 revolutions per minute. 400 Tons per hour are drawn in by the first compression stage 3 and 1046 tons per hour by the second compression stage 4.
  • the throughput of the cycle mixture is regulated by reducing the speed of rotation of the compressor 1 and by modifying the orientation of the stator blades of the second compression stage 4.
  • the power consumed by the compressor is 58.6 megawatts for a speed of rotation of 3200 revolutions per minute. 345 Tons per hour and 900 tons per hour are drawn in respectively by the compression stages 3 and 4.
  • This first recycling flow is expanded to the low pressure in the expansion valve 39, is reunited with the second refrigerating stream in the bottom of the exchanger 27 (before said stream is reheated up to ambient temperature), and is finally recompressed to the high pressure in the compressor 1 with the second vaporised refrigerating stream.
  • the combining of the first recycling flow in the circuit 35 with the second refrigerating stream is effected after the latter has been united with a part of the second condensed fraction which has been expanded in the expansion valve 29.
  • the first recycling flow is regulated from a minimum flow of zero up to a flow of the order of 3% of the reference flow of the cycle mixture (curve in solid line).
  • This second recycling flow (in the circuit 34) is then expanded in the expansion valve 33 to the intermediate pressure, and is combined with the first refrigerating stream circulating in the pipe 71 (before the latter is united with the first condensed fraction which has been explained to the intermediate pressure in the expansion valve 19, but after a part of the second condensed frac tion whichhas been expanded to the intermediate pressure in the valve 20 has been added to the first refrigerating stream).
  • The. second recycling flow is finally recompressed to the high pressure in the second compression stage 4, together with the two vaporised refrigerating streams.
  • the second recycling flow in the circuit 34 like the first recycling flow is tapped off from the residual cycle mixture, after separation of the secnd and third condensed fractions which have been collected in the separators l1 and 12 respectively. From R to R the second recycling flow, in the circuit 34, is regulated from a minimum value of zero up to a maximum'value. At the functioning point R corresponding to the liquefaction of 50% of the nominal production of liquefied natural gas (during which time the first recycling flow is at its maximum value) about 35% of the reference flow of the cycle mixture is recycled simultaneously by the circuits 34 and 35.
  • a third recycling flow is tapped off into the recycling circuit 36 at high pressure from the compressed cycle mixture circulating in the pipe 8, before the mixture undergoes partial condensation in the condenser 7 but after it has been cooled in the cooling unit 9.
  • the third recycling flow, in the circuit 36 is tapped off at the valve 40 and is then expanded to the intermediate pressure.
  • This expanded recycling flow is combined with the first refrigeration stream, which is circulating in the exchanger 14, at about the same time as the first condensed fraction (which has been expanded to the intermediate pressure in the expansion valve 19) joins said stream.
  • a fourth recycling flow at intermediate pressure is tapped off from the cycle mixture circulating in the pipe between the two compression stages 3 and 4, after the mixture has been cooled in the coolingunit 6, into the recycling circuit 37.
  • the fourth recycling flow as thus drawn off is expanded to the low pressure in the expansion valve 41, and this expanded flow is combined with the second refrigerating stream, before it is reheated to ambient temperature, in the bottom of the exchanger 24.
  • the third recycling flow (in the circuit 36) and the fourth recycling flow (in the circuit 37) are regulated and increased and simultaneously from an initial value of zero up to a final value.
  • the production of liquefied natural gas is zero, and the total recycled flow corresponds to about 80% of the reference flow of the cycle mixture which is substantially equal to the rate of flow delivered by the compressor when this latter has a speed of 3200 revolutions per minute.
  • the functioning zone contained between the positions R and R corresponds to a transient functioning TF of the refrigerating installation (starting and stopping) during which the quantity of cold delivered by the installation is regulated between an initial zero quantity (R and a final or minimum quantity (R
  • the third and fourth recycling flows, in the circuits 36 and 37, are thus simultaneously increased up to an initial rate of, flow of about 80% 0f the reference flow.
  • the installation enters a permanent functioning zone PF during which the quantity of cold delivered is regulated between the minimum quantity (R and the maximum quantity (R )
  • the first recycling flow, 35, and then the second recycling flow, in the circuit 34 are successively increased up to a maximum flow corresponding, for the two circuits 34 and 35, to a total recycled flow of 35% of the reference flow as described above.
  • the first and second recycling flows may thus be called the permanent recycling flows since their use is associated with the running of the installation under permanent conditions.
  • the second recycling flow and then the first recycling flow are successively reduced to a minimum flow of zero.
  • the recycling flows in the circuits 35 and 34 respectively are thus regulated to their maximum value during transient running periods of the installation.
  • the recycling flows 36 and 37 are first simultaneously reduced froman initialvalue to a minimum value (zero for the recycling flow in the circuit 36 but not zero for the recycling flow in the circuit 37), between the points R and R as shown in dashed lines in FIG. 2.
  • the improvement which comprises i. withdrawing at least a first gaseous recycle stream .from said cycle mixture in gaseous form, under a pressure at most equal to said higher pressure and above said lower pressure,
  • step (c) wherein by a progressive and fractional condensation according to step (c), there is obtained and separated from the residual cycle mixture at least a second and further liquid fraction, intermediate said first and last liquid fractions, and wherein said expanded gaseous portion of said first recycle stream is combined with said refrigerating stream, after at least a part of said second liquid fraction, which has been previously expanded to said vaporization pressure, is combined with said refrigerating stream.
  • step (a) said gaseous cycle mixture is cooled after being compressed according to step (a) and before being subjected to partial condensation according to step (b), and wherein said first gaseous recycle stream is drawn off at said higher pressure from said compressed cycle mixture in gaseous form before partial condensation thereof but after said compressed gaseous cycle mixture has been cooled.
  • step (0) there are obtained and separated from said residual cycle mixture second and third further liquid fractions, intermediate said first and last liquid fractions, and wherein said gaseous recycle stream is withdrawn from said residual cycle mixture in gaseous form, after the separation from said residual recycle stream of the second and third fractions.
  • step (a) compressing said cycle mixture is gaseous form according to step (a) in two compression stages separated by a conduit at a pressure intermediate said higher pressure and said lower pressure
  • step (c) progressively and fractionally condensing according to step (c), by heat exchange with a first diphasic refrigerating stream, constituting a first part of said cycle mixture, which first diphasic refrigerating stream is undergoing vaporization under a first vaporization pressure substantially equal to said intermediate pressure, and obtaining and separating from said residual cycle mixture at least a second and further liquid fraction (B), intermediate said first and last liquid fractions,
  • step (g) expanding to said first and second vaporization pressures, respectively, a first part and a second and remaining part of at least said second liquid fraction (B) of said cycle mixture, obtained during the progressive and fractional condensation according to step (g); and combining the expanded first liquid part and the expanded second liquid part thus obtained with said first diphasic refrigerating stream and with said second diphasic refrigerating stream, respectively,
  • step (g) 1. controlling withdrawal of a first permanent gaseous recycle stream from said residual cycle mixture in gaseous form during the progressive and fractional condensation of step (g) from a minimum value including a zero value up to a maximum value, said first permanent recycle stream being expanded in gaseous form to said second vaporization pressure and combined with said second diphasic refrigerating stream before said second diphasic refrigerating stream is substantially reheated to ambient temperature,
  • step (g) controlling withdrawal of a second gaseous permanent recycle stream from said residual cycle mixture in gaseous form during the progressive and fractional condensation of step (g) from another minimum value including a zero value up to another maximum value, said second permanent recycle stream being expanded in gaseous form to said first vaporization pressure and combined with said first diphasic refrigerating stream after said first diphasic refrigerating stream has been combined with said expanded first part of said second liquid fraction (B),
  • the frigorific power supplied during transient running conditions is decreased by simultaneously controlling from an initial value including a zero value up to a final value (1) a first gaseous transient recycle stream withdrawn from said compressed cycle mixture in gaseous form, after said compressed gaseous cycle mixture has been cooled but before said compressed cycle mixture is partially condensed according to step (b), then successively expanded in gaseous form to said first vaporization pressure and combined with said first diphasic refrigerating stream when said first diphasic refrigerating stream is combined with at least a part of said first liquid fraction (A) which has been expanded to said first vaporization pressure, and (2) second gaseous transient recycle stream withdrawn from said cycle mixture in gaseous form under said intermediate pressure, then successively expanded in gaseous form to said second vaporization pressure and combined with said second diphasic refrigerating stream before said second diphasic refrigerating stream is substantially reheated up to ambient temperature.

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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4037426A (en) * 1975-06-09 1977-07-26 Institut Francais Du Petrole Cold producing process
US4228660A (en) * 1977-03-16 1980-10-21 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Heat exchangers
AU688218B2 (en) * 1995-04-18 1998-03-05 Shell Internationale Research Maatschappij B.V. Cooling a fluid stream
EP0893665A2 (en) * 1997-07-24 1999-01-27 Air Products And Chemicals, Inc. Method and apparatus for regulatory control of production and temperature in a mixed refrigerant liquefied natural gas facility
US20130205813A1 (en) * 2010-12-03 2013-08-15 Mitsubishi Electric Corporation Method of part replacement for refrigeration cycle apparatus
WO2019126832A1 (en) * 2017-12-21 2019-06-27 Shell Oil Company System and method for operating a liquefaction train

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2628007A1 (de) * 1976-06-23 1978-01-05 Heinrich Krieger Verfahren und anlage zur erzeugung von kaelte mit wenigstens einem inkorporierten kaskadenkreislauf
US6308531B1 (en) 1999-10-12 2001-10-30 Air Products And Chemicals, Inc. Hybrid cycle for the production of liquefied natural gas

Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2551666A (en) * 1948-05-24 1951-05-08 Phillips Petroleum Co Continuous removal of impurities from refrigerant during a refrigeration process
US3212276A (en) * 1961-08-17 1965-10-19 Gulf Oil Corp Employing the heating and cooling effect of a refrigerating cycle
US3213631A (en) * 1961-09-22 1965-10-26 Lummus Co Separated from a gas mixture on a refrigeration medium
US3299646A (en) * 1964-06-17 1967-01-24 Little Inc A Cryogenic joule-thomson helium liquefier with cascade helium and nitrogen refrigeration circuits
US3348384A (en) * 1965-02-19 1967-10-24 Conch Int Methane Ltd Process for the partial liquefaction of a gas mixture
US3364685A (en) * 1965-03-31 1968-01-23 Cie Francaise D Etudes Et De C Method and apparatus for the cooling and low temperature liquefaction of gaseous mixtures
US3593535A (en) * 1965-06-29 1971-07-20 Air Prod & Chem Liquefaction of natural gas employing multiple-component refrigerants
US3742721A (en) * 1970-01-08 1973-07-03 Technip Cie Method of regulation of the temperature of the liquefied gas or gaseous mixture in an apparatus for the liquefaction of gaseous fluids
US3747360A (en) * 1970-02-12 1973-07-24 Fr D Etudes Et De Construction Cooling and low temperature liquefaction of gaseous mixtures with multicomponent refrigerant
US3808826A (en) * 1970-09-28 1974-05-07 Phillips Petroleum Co Refrigeration process
US3817046A (en) * 1970-11-28 1974-06-18 Chinzoda Chem Eng & Constructi Absorption-multicomponent cascade refrigeration for multi-level cooling of gas mixtures

Patent Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2551666A (en) * 1948-05-24 1951-05-08 Phillips Petroleum Co Continuous removal of impurities from refrigerant during a refrigeration process
US3212276A (en) * 1961-08-17 1965-10-19 Gulf Oil Corp Employing the heating and cooling effect of a refrigerating cycle
US3213631A (en) * 1961-09-22 1965-10-26 Lummus Co Separated from a gas mixture on a refrigeration medium
US3299646A (en) * 1964-06-17 1967-01-24 Little Inc A Cryogenic joule-thomson helium liquefier with cascade helium and nitrogen refrigeration circuits
US3348384A (en) * 1965-02-19 1967-10-24 Conch Int Methane Ltd Process for the partial liquefaction of a gas mixture
US3364685A (en) * 1965-03-31 1968-01-23 Cie Francaise D Etudes Et De C Method and apparatus for the cooling and low temperature liquefaction of gaseous mixtures
US3593535A (en) * 1965-06-29 1971-07-20 Air Prod & Chem Liquefaction of natural gas employing multiple-component refrigerants
US3645106A (en) * 1965-06-29 1972-02-29 Lee S Gaumer Jr Process for liquefying natural gas employing a multicomponent refrigerant for obtaining low temperature cooling
US3742721A (en) * 1970-01-08 1973-07-03 Technip Cie Method of regulation of the temperature of the liquefied gas or gaseous mixture in an apparatus for the liquefaction of gaseous fluids
US3747360A (en) * 1970-02-12 1973-07-24 Fr D Etudes Et De Construction Cooling and low temperature liquefaction of gaseous mixtures with multicomponent refrigerant
US3808826A (en) * 1970-09-28 1974-05-07 Phillips Petroleum Co Refrigeration process
US3817046A (en) * 1970-11-28 1974-06-18 Chinzoda Chem Eng & Constructi Absorption-multicomponent cascade refrigeration for multi-level cooling of gas mixtures

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4037426A (en) * 1975-06-09 1977-07-26 Institut Francais Du Petrole Cold producing process
US4228660A (en) * 1977-03-16 1980-10-21 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Heat exchangers
AU688218B2 (en) * 1995-04-18 1998-03-05 Shell Internationale Research Maatschappij B.V. Cooling a fluid stream
US5832745A (en) * 1995-04-18 1998-11-10 Shell Oil Company Cooling a fluid stream
EP0893665A2 (en) * 1997-07-24 1999-01-27 Air Products And Chemicals, Inc. Method and apparatus for regulatory control of production and temperature in a mixed refrigerant liquefied natural gas facility
EP0893665A3 (en) * 1997-07-24 1999-06-09 Air Products And Chemicals, Inc. Method and apparatus for regulatory control of production and temperature in a mixed refrigerant liquefied natural gas facility
US20130205813A1 (en) * 2010-12-03 2013-08-15 Mitsubishi Electric Corporation Method of part replacement for refrigeration cycle apparatus
US9279607B2 (en) * 2010-12-03 2016-03-08 Mitsubishi Electric Corporation Method of part replacement for refrigeration cycle apparatus
WO2019126832A1 (en) * 2017-12-21 2019-06-27 Shell Oil Company System and method for operating a liquefaction train
AU2019204704B2 (en) * 2017-12-21 2021-07-01 Shell Internationale Research Maatschappij B.V. System and method for operating a liquefaction train

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JPS5727373B2 (xx) 1982-06-10
JPS49100630A (xx) 1974-09-24
FR2201444A1 (xx) 1974-04-26
AU6050573A (en) 1975-03-20
FR2201444B1 (xx) 1977-01-14

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